A METHOD FOR REVAMPING A CO2 REMOVAL SECTION FOR PURIFICATION OF A HYDROGEN-CONTAINING GAS

A method for revamping a CO2 removal section for removing carbon dioxide from a hydrogen-containing synthesis gas, wherein the CO2 removal section comprises an absorption section () wherein carbon dioxide is transferred to an absorbing solution and a stripping tower () for regeneration of the CO2-loaded solution, said stripping tower comprising an upper zone () where a first gaseous CO2 stream () and a partially regenerated semi-lean solution () are produced, and a lower zone () acting as a stripping zone where a second gaseous CO2 stream () and a lean regenerated solution are produced, the second CO2 stream () being a substantially pure stream containing less hydrogen and impurities than the first CO2 stream, and wherein the method of revamping provides the installation of sealing means () inside the stripping tower (), arranged to isolate said second gaseous CO2 stream () from the first stream (), so that the second stream () can be exported separately. 1) A method for revamping a CO2 removal section for removing carbon dioxide from a hydrogen-containing synthesis gas , wherein:{'b': 1', '2', '6', '7', '8, 'said CO2 removal section () comprises an absorption section () wherein carbon dioxide is removed from the synthesis gas () by absorption in an absorbing solution (), obtaining a CO2-rich solution (), and'}{'b': 3', '8', '4', '10', '11', '5', '11', '12', '13, 'a stripper () for regeneration of the CO2-rich solution (), comprising an upper zone () where said solution coming from the absorber is flashed producing a first gaseous stream () containing CO2 and a partially regenerated semi-lean solution (), and a lower zone () acting as a stripping zone where the semi-lean solution () is stripped producing a second gaseous stream () containing CO2 and a lean regenerated solution (),'}{'b': 12', '10, 'said second gaseous stream () having a hydrogen content which is lower than the hydrogen content of said first gaseous stream (),'}the method of revamping being ...

Process for producing ammonia synthesis gas

A process for producing ammonia synthesis gas from a hydrocarbon-containing feedstock, with steps of primary reforming, secondary reforming with an oxidant stream, and further treatment of the synthesis gas including shift, removal of carbon dioxide and methanation, wherein the synthesis gas delivered by secondary reforming is subject to a medium-temperature shift (MTS) at a temperature between 200 and 350° C., and primary reforming is operated with a steam-to-carbon ratio lower than 2. A corresponding method for revamping an ammonia plant is disclosed, where an existing HTS reactor is modified to operate at medium temperature, or replaced with a new MTS reactor, and the steam-to-carbon ratio in the primary reformer is lowered to a value in the range 1-5−2, thus reducing inert steam in the flow rate trough the equipments of the front-end.

Process for Selective Removal of a Product from a Gaseous System

A process for selective removal of a gaseous product (P) from a gaseous system comprising said product and other components (R 1 , R 2 ), wherein the gaseous system is admitted to a first environment, which is separated from a second environment by a boundary wall, and a permeation membrane ( 3, 300 ) forms at least part of said boundary wall; a spatially non-uniform electric field ( 4 ) is generated between a first electrode or first plurality of electrodes ( 1, 301 ) located in the first environment and a second electrode or second plurality of electrodes ( 2, 302 ) located in the second environment, so that field lines of said non-uniform electric field cross said membrane, and a dielectrophoretic force generated on particles of said gaseous component (P) is at least part of a driving force of the permeation through said membrane, an amount of said product (P) being selectively removed from the first environment and collected in the second environment.

PROCESS AND EQUIPMENT FOR THE PRODUCTION OF AMMONIA MAKE-UP SYNGAS WITH AN AIR SEPARATION UNIT AS NITROGEN SOURCE

A process and a plant for producing a makeup synthesis gas ( 6 ) for the synthesis of ammonia where a hydrocarbon feedstock is reformed in a primary reformer ( 10 ) and in an autothermal reformer ( 14 ) in parallel with said primary reformer; nitrogen is furnished by an air separation unit ( 13 ), and O 2 -enhched air ( 8 ) produced in said air separation unit is fed to the autothermal reformer. A method for the revamping of the front-end of an ammonia plant is also disclosed.

Multi-bed catalytic converter

A multi-bed catalytic converter comprising: a plurality of catalytic beds which are traversed in series by a process gas, sequentially from a first catalytic bed to a last catalytic bed of said plurality, and at least one inter-bed heat exchanger (7) positioned between a first catalytic bed and a second catalytic bed of said plurality, wherein at least the last catalytic bed of said plurality is adiabatic and is made of fine catalyst with a particle size not greater than 2 mm.

Method for revamping an ammonia plant

A method for revamping an ammonia plant including a steam system, said steam system comprising at least a high-pressure section operating at a first pressure and a medium-pressure section operating at a second pressure lower than said first pressure, the revamping including: the provision of at least one additional heat recovery by means of a steam flow at a third pressure which is intermediate between said first and second pressure, and the provision of a steam export line arranged to export outside the ammonia plant at least a portion of said steam flow at said third pressure.

Process and equipment for the production of ammonia make-up syngas with an air separation unit as nitrogen source

A process and a plant for producing a makeup synthesis gas (6) for the synthesis of ammonia where a hydrocarbon feedstock is reformed in a primary reformer (10) and in an autothermal reformer (14) in parallel with said primary reformer; nitrogen is furnished by an air separation unit (13), and O2-enhched air (8) produced in said air separation unit is fed to the autothermal reformer. A method for the revamping of the front-end of an ammonia plant is also disclosed.

Process for the synthesis of ammonia

A dual pressure process for the synthesis of ammonia from a make-up gas, wherein the make-up gas is reacted in two steps in series, the second step operating at a greater pressure than the first step, and wherein a portion of the effluent of the first step is recycled back to the first step, said portion containing unreacted make-up gas.

Recovery of CO2 in a process for the synthesis of methanol

A process for producing methanol, where a hydrocarbon feedstock (1) is reformed and a make-up syngas is reacted in a synthesis loop, obtaining crude methanol which is further treated to obtain high-grade methanol, and where the carbon dioxide dissolved in the crude methanol is recycled to the reforming section in order to adjust the stoichiometric number of the make-up syngas. In a preferred embodiment, a flash gas (9) separated from the crude methanol (8) and light ends (10) coming from distillation are recycled to a compressor (106) and fed to a primary reformer (100); further carbon dioxide can be recycled from the flue gas (11).

Method for increasing the capacity of an ammonia plant

A method for treatment of process condensate (1) in an ammonia plant, wherein the ammonia plant comprises a front-end section producing a make-up gas and a synthesis section where the make-up gas is reacted to ammonia, and said process condensate (1) is collected from one or more equipment of the ammonia plant and is an aqueous solution comprising ammonia, carbon dioxide and methanol. Said method comprises: stripping said process condensate with low-pressure steam (4), obtaining a vapour phase (5) comprising ammonia, carbon dioxide and methanol stripped from the process condensate; condensing said vapour phase, obtaining a solution (11) enriched of ammonia and methanol; re-introducing a first portion (12) of said solution to said stripping environment; recycling a second portion (13) of said solution to said ammonia plant.

MULTI-BED CATALYTIC CONVERTER WITH INTER-BED COOLING

A multi-bed catalytic converter comprising at least a first catalytic bed, a second catalytic bed and a heat exchanger arranged between said first bed and said second bed, wherein said heat exchanger is arranged to transfer heat from the hot effluent of the first bed to a cooling medium; said heat exchanger comprises a plurality of stacked round plates, wherein adjacent plates define gaps therebetween, and the effluent of the first catalytic bed and the cooling medium are respectively fed into alternate gaps. 124-. (canceled)25. A multi-bed cylindrical catalytic converter , comprising:a first catalytic bed;a second catalytic bed;a heat exchanger arranged between said first catalytic bed and said second catalytic bed, said heat exchanger being arranged to transfer heat from a first medium to a second medium;an input and an output for the first medium; andan input and an output for the second medium;wherein the first medium is the hot effluent of the first catalytic bed before admission into the second catalytic bed, and the second medium is a cooling medium;wherein said heat exchanger comprises a plurality of stacked round plates, said plurality of stacked round plates being full circular plates or annular plates, and adjacent plates of the plurality of stacked round rates define gaps therebetween;wherein the hot effluent of the first catalytic bed and the cooling medium pass respectively through alternating ones of the gaps between the plurality of stacked round plates;wherein said first catalytic bed is a hollow cylinder comprising a cavity and said heat exchanger is arranged coaxially to the first catalytic bed inside said cavity.26. The multi-bed cylindrical catalytic converter according to claim 25 , wherein said plurality of stacked round plates are stamped plates obtained mechanically by metal sheet pressing.27. The multi-bed cylindrical catalytic converter according to claim 25 , wherein at least one of the input or the output of at least one of the first ...

PROCESS FOR PRODUCING AMMONIA SYNTHESIS GAS

A process for producing ammonia synthesis gas from a hydrocarbon-containing feedstock, with steps of primary reforming, secondary reforming with an oxidant stream, and further treatment of the synthesis gas including shift, removal of carbon dioxide and methanation, wherein the synthesis gas delivered by secondary reforming is subject to a medium-temperature shift (MTS) at a temperature between 200 and 350.degree. C., and primary reforming is operated with a steam-to-carbon ratio lower than 2. A corresponding method for revamping an ammonia plant is disclosed, where an existing HTS reactor is modified to operate at medium temperature, or replaced with a new MTS reactor, and the steam-to-carbon ratio in the primary reformer is lowered to a value in the range 1-5-2, thus reducing inert steam in the flow rate trough the equipments of the front-end.

A METHOD FOR INCREASING THE CAPACITY OF AN AMMONIA PLANT

A method for treatment of process condensate () in an ammonia plant, wherein the ammonia plant comprises a front-end section producing a make-up gas and a synthesis section where the make-up gas is reacted to ammonia, and said process condensate () is collected from one or more equipment of the ammonia plant and is an aqueous solution comprising ammonia, carbon dioxide and methanol. Said method comprises: stripping said process condensate with low-pressure steam (), obtaining a vapour phase () comprising ammonia, carbon dioxide and methanol stripped from the process condensate; condensing said vapour phase, obtaining a solution () enriched of ammonia and methanol; re-introducing a first portion () of said solution to said stripping environment; recycling a second portion () of said solution to said ammonia plant. 1. A method for treatment of process condensate in an ammonia plant , wherein:the ammonia plant comprises a front-end section producing a make-up gas from reforming of a hydrocarbon source, and a synthesis section where the make-up gas is reacted to ammonia;said process condensate is collected from one or more equipment of the ammonia plant and is an aqueous solution comprising ammonia, carbon dioxide and methanol,the method comprising:stripping of said process condensate in a stripping environment with low-pressure steam having a pressure of no more than 10 bar, obtaining a vapour phase comprising ammonia, carbon dioxide and methanol stripped from the process condensate;condensing said vapour phase, obtaining a condensate solution enriched of ammonia and methanol;re-introducing a first portion of said condensate solution to said stripping environment wherein said first portion of solution is reintroduced directly into said stripping environment;recycling a second portion of said condensate solution to said ammonia plant, wherein said second portion is no more than 4% by volume of said condensate solution.2. The method according to claim 1 , wherein the ...

A METHOD FOR REVAMPING AN AMMONIA PLANT

A method for revamping an ammonia plant including a steam system, said steam system comprising at least a high-pressure section operating at a first pressure and a medium-pressure section operating at a second pressure lower than said first pressure, the revamping including: the provision of at least one additional heat recovery by means of a steam flow at a third pressure which is intermediate between said first and second pressure, and the provision of a steam export line arranged to export outside the ammonia plant at least a portion of said steam flow at said third pressure. 1. A method for revamping an ammonia plant including a steam system , said steam system comprising at least a high-pressure section operating at a first pressure and a medium-pressure section operating at a second pressure lower than said first pressure ,the revamping including:the provision of at least one additional heat recovery by means of a steam flow at a third pressure which is intermediate between said first and second pressure, andthe provision of a steam export line arranged to export outside the ammonia plant at least a portion of said steam flow at said third pressure.2. The method according to claim 1 , wherein:said ammonia plant is part of an installation including other ammonia plants, andsaid steam is exported to another ammonia plant of the installation, having a medium-pressure steam section operating at said third pressure.3. The method according to claim 2 , including:the installation of a new high-pressure steam user in the high-pressure section of the steam system, said steam user having a steam input taken from the high-pressure section, and said steam flow at intermediate pressure being taken from a steam outlet of said new steam user.4. The method according to claim 3 , wherein operation of an existing medium-pressure steam user of the steam system is discontinued claim 3 , and the discontinued steam user is replaced by said new high-pressure steam user.5. The method ...

Process for revamping an ammonia plant with nitrogen-based washing of a purge stream

A process and a plant for producing ammonia, where an ASU ( 3 ) delivers an oxygen stream and a nitrogen stream; the oxygen stream ( 9 ) is fed to the secondary reformer of a front-end reforming section ( 1 ); the nitrogen stream ( 10 ) is used to wash a purge gas or tail gas taken from the synthesis loop ( 2 ), preferably in a cryogenic section; a methane-free and inert-free gas stream is recovered and recycled to the synthesis loop ( 2 ) or at the suction of the main syngas compressor, to recover the hydrogen contained therein. A corresponding method for increasing the capacity of an ammonia plant, by providing the ASU and feeding the oxygen stream to the secondary reformer and the nitrogen stream to a suitable purge gas recovery unit.

Process for selective removal of a product from a gaseous system

A process for selective removal of a gaseous product (P) from a gaseous system comprising said product and other components (R1, R2), wherein the gaseous system is admitted to a first environment, which is separated from a second environment by a boundary wall, and a permeation membrane (3, 300) forms at least part of said boundary wall; a spatially non-uniform electric field (4) is generated between a first electrode or first plurality of electrodes (1, 301) located in the first environment and a second electrode or second plurality of electrodes (2, 302) located in the second environment, so that field lines of said non-uniform electric field cross said membrane, and a dielectrophoretic force generated on particles of said gaseous component (P) is at least part of a driving force of the permeation through said membrane, an amount of said product (P) being selectively removed from the first environment and collected in the second environment.

A PLANT, SUCH AS AMMONIA PLANT, COMPRISING AN ABSORPTION REFRIGERATION UNIT

A chemical plant comprising a refrigeration system including an absorption refrigeration unit, and a steam system including one or more steam producers, steam users, and at least one steam condenser, wherein a heat exchanger is arranged to intercept at least part of a steam flow directed to said steam condenser, and said heat exchanger transfers heat to a working fluid of said absorption refrigeration unit to provide at least part of a heat input required for operation of said refrigeration system. 114-. (canceled)15. A chemical plant , comprising:a refrigeration system including at least an absorption refrigeration unit;a steam system including one or more steam producers, steam users, and at least one steam condenser; anda heat exchanger is arranged to intercept at least part of a steam flow directed to said steam condenser; said heat exchanger transfers heat to a working fluid of said at least one absorption refrigeration unit to provide at least part of a heat input required for operation of said refrigeration system.16. The chemical plant of claim 15 , wherein said heat exchanger is fitted within a steam duct directed to said at least one steam condenser.17. The chemical plant of claim 15 , wherein said heat exchanger includes a coil or tube bundle exposed to the steam and internally traversed by said working fluid.18. The chemical plant of claim 15 , wherein steam at an inlet of said heat exchanger has a temperature in a range of 60 to 90° C claim 15 ,.19. The chemical plant of claim 18 , wherein the temperature is in a range of 75 to 85° C.20. The chemical plant of claim 15 , wherein said working fluid of the at least one absorption refrigeration unit includes a binary solution of a refrigerant and an absorbent.21. The chemical plant of claim 20 , wherein said binary solution includes lithium bromide and water.22. The chemical plant of claim 15 , which is suitable for synthesis of ammonia and further comprising:a front-end section for generation of a make-up ...

MULTI-BED CATALYTIC CONVERTER

A multi-bed catalytic converter comprising: a plurality of catalytic beds which are traversed in series by a process gas, sequentially from a first catalytic bed to a last catalytic bed of said plurality, and at least one inter-bed heat exchanger () positioned between a first catalytic bed and a second catalytic bed of said plurality, wherein at least the last catalytic bed of said plurality is adiabatic and is made of fine catalyst with a particle size not greater than 2 mm. 115-. (canceled)16. A multi-bed catalytic converter , comprising:a plurality of catalytic beds which are traversed in series by a process gas, sequentially from a first catalytic bed to a last catalytic bed of said plurality of catalytic beds; andat least one inter-bed heat exchanger positioned between the first catalytic bed and a second catalytic bed of said plurality of catalytic beds, and arranged to remove heat from the process gas leaving the first catalytic bed before entering the second catalytic bed;wherein at least the last catalytic bed of said plurality of catalytic beds is adiabatic and is made of a fine catalyst with a particle size not greater than 2 mm;wherein each of the plurality of catalytic beds includes at least one gas distributor and at least one gas collector arrange to provide that the catalytic bed is traversed by the process gas with a radial flow or axial-radial flow.17. The multi-bed catalytic converter of claim 16 , wherein the particle size of said fine catalyst is 0.8 mm to 1.4 mm.18. The multi-bed catalytic converter of claim 17 , wherein the particle size is 0.8 mm to 1.4 mm.19. The multi-bed catalytic converter of claim 16 , wherein said fine catalyst has a particle size of 1.3 mm or about 1.3 mm.20. The multi-bed catalytic converter of claim 16 , wherein only the last catalytic bed of said plurality of catalytic beds is made of fine catalyst claim 16 , the other catalytic bed(s) of the plurality of catalytic beds being made of catalyst with greater particle ...

RECOVERY OF CO2 IN A PROCESS FOR SYNTHESIS OF METHANOL

A process for producing methanol, where a hydrocarbon feedstock (1) is reformed and a make-up syngas is reacted in a synthesis loop, obtaining crude methanol which is further treated to obtain high-grade methanol, and where the carbon dioxide dissolved in the crude methanol is recycled to the reforming section in order to adjust the stoichiometric number of the make-up syngas. In a preferred embodiment, a flash gas (9) separated from the crude methanol (8) and light ends (10) coming from distillation are recycled to a compressor (106) and fed to a primary reformer (100); further carbon dioxide can be recycled from the flue gas (11).

Method for revamping a CO2 removal section for purification of a hydrogen-containing gas

A method for revamping a CO2 removal section for removing carbon dioxide from a hydrogen-containing synthesis gas, wherein the CO2 removal section comprises an absorption section (2) wherein carbon dioxide is transferred to an absorbing solution and a stripping tower (3) for regeneration of the CO2-loaded solution, said stripping tower comprising an upper zone (4) where a first gaseous CO2 stream (10) and a partially regenerated semi-lean solution (11) are produced, and a lower zone (5) acting as a stripping zone where a second gaseous CO2 stream (12) and a lean regenerated solution are produced, the second CO2 stream (12) being a substantially pure stream containing less hydrogen and impurities than the first CO2 stream, and wherein the method of revamping provides the installation of sealing means (16) inside the stripping tower (3), arranged to isolate said second gaseous CO2 stream (12) from the first stream (10), so that the second stream (12) can be exported separately.

PROCESS FOR REVAMPING AN AMMONIA PLANT WITH NITROGEN-BASED WASHING OF A PURGE STREAM

A process and a plant for producing ammonia, where an ASU () delivers an oxygen stream and a nitrogen stream; the oxygen stream () is fed to the secondary reformer of a front-end reforming section (); the nitrogen stream () is used to wash a purge gas or tail gas taken from the synthesis loop (), preferably in a cryogenic section; a methane-free and inert-free gas stream is recovered and recycled to the synthesis loop () or at the suction of the main syngas compressor, to recover the hydrogen contained therein. A corresponding method for increasing the capacity of an ammonia plant, by providing the ASU and feeding the oxygen stream to the secondary reformer and the nitrogen stream to a suitable purge gas recovery unit. 1. A process for producing ammonia , comprising the steps of:{'sub': '2', 'producing a make-up syngas by steam reforming of a hydrocarbon source, the steam reforming comprising steps of primary reforming and secondary reforming, and further treatment steps of shift, COremoval and methanation;'}compressing and reacting the make-up syngas in a high-pressure synthesis loop to produce ammonia;subjecting an air feed to a separation process into an oxygen stream and at least one nitrogen stream, wherein said oxygen stream provides additional oxidizer to said secondary reforming; andcontacting a purge gas stream, which is a purge gas purged from said synthesis loop or a tail gas coming from a purge gas recovery section, and which contains inerts, with a nitrogen stream obtained from said air separation process, said nitrogen stream being in a liquid or gaseous state, or a mixture of liquid and gaseous nitrogen, obtaining a hydrogen-containing and substantially inert-free recycle gas stream, and said recycle gas stream is recycled to the synthesis loop.23-. (canceled)4. The process according to claim 1 , wherein said purge gas stream is contacted with said nitrogen stream at a cryogenic temperature claim 1 , and wherein upon contacting with the nitrogen ...

PROCESS FOR THE SYNTHESIS OF AMMONIA

A dual pressure process for the synthesis of ammonia from a make-up gas, wherein the make-up gas is reacted in two steps in series, the second step operating at a greater pressure than the first step, and wherein a portion of the effluent of the first step is recycled back to the first step, said portion containing unreacted make-up gas. 111) A process for the synthesis of ammonia from a make-up gas () , the process comprising a first reactive step at a first pressure (P) and a second reactive step at a second pressure (P) greater than the first pressure , wherein:{'b': 14', '15, 'the first reactive step provides a product stream () containing ammonia and a gaseous effluent () containing unreacted make-up gas;'}{'b': 16', '16, 'i': 'a', 'a first portion (, ) of said gaseous effluent is subjected to said second reactive step, and'}{'b': 15', '16, 'i': b,', 'b, 'a second portion () of said gaseous effluent is recycled to said first reactive step.'}21516b,b) A process according to claim 1 , comprising a step of compression of the gaseous effluent of the first reactive step from said first pressure (P) to said second pressure (P) claim 1 , and the second portion () of said gaseous effluent being taken before or after said step of compression.3156b) A process according to claim 2 , wherein said second portion () is taken before said step of compression and is recycled to said first reactive step through an ejector ().4116) A process according to claim 3 , wherein said make-up gas () works as motive fluid inside said ejector ().51115613b) A process according to claim 4 , wherein said make-up gas () mixes with said second portion () inside the ejector () forming the input stream () to said first reactive step.616b) A process according to claim 2 , wherein said second portion () is taken after said step of compression and is recycled directly to said first reactive step.7161123b) Process according to claim 6 , wherein said second portion () mixes with said make-up gas () ...

Process for Producing Ammonia Synthesis Gas

A process for producing ammonia synthesis gas from a hydrocarbon-containing feedstock, with steps of primary reforming, secondary reforming with an oxidant stream, and further treatment of the synthesis gas including shift, removal of carbon dioxide and methanation, wherein the synthesis gas delivered by secondary reforming is subject to a medium-temperature shift (MTS) at a temperature between 200 and 350° C., and primary reforming is operated with a steam-to-carbon ratio lower than 2. A corresponding method for revamping an ammonia plant is disclosed, where an existing HTS reactor is modified to operate at medium temperature, or replaced with a new MTS reactor, and the steam-to-carbon ratio in the primary reformer is lowered to a value in the range 1-5-2, thus reducing inert steam in the flow rate trough the equipments of the front-end. 1. A process for producing ammonia synthesis gas from a hydrocarbon-containing feedstock , the process comprising the steps of primary reforming said feedstock with steam , secondary reforming with an oxidant stream , and further treatment of the synthesis gas involving at least shift , removal of carbon dioxide and methanation , the process being characterized in that:the synthesis gas produced by said secondary reforming is subject to a medium-temperature shift at a temperature between 200 and 350° C.,and in that said primary reforming is operated with a steam-to-carbon ratio lower than 2.2. A process according to claim 1 , said steam-to-carbon ratio being 1.5 to 2 and preferably 1.5 to 1.7.3. A process according to or claim 1 , comprising a step of pre-reforming of said feedstock before the step of primary reforming.4. A process according to any of to claim 1 , said oxidant stream being any of air claim 1 , O-enriched air or substantially pure oxygen.5. A process according to any of to claim 1 , said medium-temperature shift being carried out in a substantially isothermal condition claim 1 , by removing heat with a suitable ...

Multi-bed catalytic converter with inter-bed cooling

A multi-bed catalytic converter comprising at least a first catalytic bed, a second catalytic bed and a heat exchanger arranged between said first bed and said second bed, wherein said heat exchanger is arranged to transfer heat from the hot effluent of the first bed to a cooling medium; said heat exchanger comprises a plurality of stacked round plates, wherein adjacent plates define gaps therebetween, and the effluent of the first catalytic bed and the cooling medium are respectively fed into alternate gaps.

RADIAL OR AXIAL-RADIAL CHEMICAL REACTOR WITH A FINE CATALYST

Reactor for catalytic chemical reactions comprising a catalyst bed with an annular-cylindrical form crossed by a radial flow or mixed axial-radial flow, wherein the bed is delimited by cylindrical walls made gas-permeable by means of slits and the catalyst bed is formed by particles of catalyst with a nominal minimum size such that: the ratio between a transverse dimension of the slits and the nominal minimum size of the particles of catalyst is smaller than or equal to 0.6; the catalyst bed contains no more than 3% by weight of particles with an actual size smaller than said nominal size. 111-. (canceled)12. A reactor for catalytic chemical reactions , the reactor comprising:a catalyst bed with an annular-cylindrical form and a radial or mixed axial-radial crossing flow;at least a first cylindrical wall and a second cylindrical wall that delimit the catalyst bed being in direct with the catalyst, the second cylindrical wall being coaxial and internal relative to the first wall;wherein the first wall and the second wall include passages to make the first and second walls gas-permeable;wherein the passages are slits having an elongated form in a longitudinal direction of the slit and a respective transverse dimension in a transverse direction that is perpendicular to the longitudinal direction;wherein the catalyst bed is formed by particles of catalyst that have a nominal minimum size such that:a) a ratio between the transverse dimension of the slits and the nominal minimum size of the particles of catalyst is less than or equal to 0.6; 'wherein a minimum size of the catalyst is defined as a square root of a maximum square free flow area of a sieve that retains the catalyst, the sieving of the catalyst being performed according to the standard test method of ASTM D4513-11.', 'b) the catalyst bed contains no more than 3% by weight of particles with a size smaller than the nominal size,'}13. The reactor according to claim 12 , wherein the nominal minimum size of the ...

A PERFORATED-TRAY COLUMN AND A METHOD OF REVAMPING THE SAME

A perforated-tray column wherein each tray comprises downcomer pipes for conveying a downwardly flowing liquid to a next tray, wherein the downcomer pipe includes: a first portion extending above the perforated tray, a second portion extending below the perforated tray towards the next perforated tray, and an end guard to prevent a gaseous phase from entering the downward pipe. 115-. (canceled)16. A perforated-tray column for the interaction of a downwardly flowing liquid with an ascending gaseous stream , the perforated-tray column comprising:a vessel with a vertical axis; and a first portion extending above the first perforated tray; and', 'a second portion extending below the first perforated tray towards the second perforated tray;', 'wherein the first portion terminates with an inlet section of the downcomer pipe located above the first perforated tray;', 'wherein the second portion terminates above the second perforated tray with an outlet section and an end guard;', 'wherein the end guard is configured to maintain the outlet section submerged by the liquid flowing through the downcomer pipe; and', 'wherein each of the plurality of downcomer pipes associated to the first perforated tray is axially aligned with a corresponding one of the plurality of downcomer pipes associated to the second perforated tray., 'a perforated tray assembly including at least a first perforated tray and a second perforated tray which is next to and below the first perforated tray, the first perforated tray includes a plurality of downcomer pipes, wherein each of the plurality of downcomer pipes includes17. The perforated-tray column according to claim 16 , wherein the second portion of downcomer pipes of the first perforated tray terminates above the second perforated tray at a distance from the second perforated tray that is greater than a height of first portions of downcomer pipes of the second tray.18. The perforated-tray column according to claim 16 , wherein the inlet section ...

Recovery of CO2 in a Process for the Synthesis of Methanol

A process for producing methanol, where a hydrocarbon feedstock () is reformed and a make-up syngas is reacted in a synthesis loop, obtaining crude methanol which is further treated to obtain high-grade methanol, and where the carbon dioxide dissolved in the crude methanol is recycled to the reforming section in order to adjust the stoichiometric number of the make-up syngas. In a preferred embodiment, a flash gas () separated from the crude methanol () and light ends () coming from distillation are recycled to a compressor () and fed to a primary reformer (); further carbon dioxide can be recycled from the flue gas (). 1. A process for producing methanol , comprising the steps of:a. reforming a hydrocarbon feedstock in a reforming process step, obtaining a make-up syngas comprising carbon oxides and hydrogen;b. reacting said make-up syngas in a methanol synthesis loop, obtaining crude methanol;c. processing said crude methanol to obtain methanol of a required purity;{'sub': '2', 'd. recovering at least one CO-rich stream from the processing of said crude methanol, and'}{'sub': '2', 'e. recycling said at least one CO-rich stream as an input stream for said reforming process step.'}2. The process according to claim 1 , where said step d) of recovering a CO-rich stream from the crude methanol comprises the recovering of a flash gas stream released by de-pressurization of the crude methanol.3. The process according to claim 1 , where said step d) of recovering a CO-rich stream from the crude methanol comprises the recovering of a gas stream containing carbon dioxide released by the crude methanol in a distillation process.4. The process according to claim 1 , where{'sub': '2', 'where said step d) of recovering a CO-rich stream from the crude methanol comprises the recovering of a flash gas stream released by de-pressurization of the crude methanol and comprises the recovering of a light-ends gas stream containing carbon dioxide released by the crude methanol in a ...

Multi-bed catalytic converter

A multi-bed catalytic converter comprising: a plurality of catalytic beds (4, 5, 6) which are traversed in series by a process gas, sequentially from a first catalytic bed (4) to a last catalytic bed (6) of said plurality, and at least one inter-bed heat exchanger (7) positioned between a first catalytic bed (4) and a second catalytic bed (5) of said plurality, wherein at least the last catalytic bed (6) of said plurality is adiabatic and is made of fine catalyst with a particle size not greater than 2 mm.

co2 recovery in a process for methanol synthesis

A method for revamping an ammonia plant

A method for revamping an ammonia plant including a steam system, said steam system comprising at least a high-pressure section operating at a first pressure and a medium-pressure section operating at a second pressure lower than said first pressure, the revamping including: the provision of at least one additional heat recovery by means of a steam flow at a third pressure which is intermediate between said first and second pressure, and the provision of a steam export line arranged to export outside the ammonia plant at least a portion of said steam flow at said third pressure.

A method for increasing the capacity of an ammonia plant

A method for treatment of process condensate (1) in an ammonia plant, wherein the ammonia plant comprises a front-end section producing a make-up gas and a synthesis section where the make-up gas is reacted to ammonia, and said process condensate (1) is collected from one or more equipment of the ammonia plant and is an aqueous solution comprising ammonia,carbon dioxide and methanol. Said method comprises: stripping said process condensate with low-pressure steam (4), obtaining a vapour phase (5) comprising ammonia, carbon dioxide and methanol stripped from the process condensate; condensing said vapour phase, obtaining a solution (11) enriched of ammonia and methanol; re-introducing a first portion (12) of said solution to said stripping environment; recycling a second portion (13) of said solution to said ammonia plant.

A method for increasing the capacity of an ammonia plant

A method for treatment of process condensate (1) in an ammonia plant, wherein the ammonia plant comprises a front-end section producing a make-up gas and a synthesis section where the make-up gas is reacted to ammonia, and said process condensate (1) is collected from one or more equipment of the ammonia plant and is an aqueous solution comprising ammonia,carbon dioxide and methanol. Said method comprises: stripping said process condensate with low-pressure steam (4), obtaining a vapour phase (5) comprising ammonia, carbon dioxide and methanol stripped from the process condensate; condensing said vapour phase, obtaining a solution (11) enriched of ammonia and methanol; re-introducing a first portion (12) of said solution to said stripping environment; recycling a second portion (13) of said solution to said ammonia plant.

A process for selective removal of a product from a gaseous system

A process for selective removal of a gaseous product (P) from a gaseous system comprising said product and other components (R1, R2), wherein the gaseous system is admitted to a first environment, which is separated from a second environment by a boundary wall, and a permeation membrane (3, 300) forms at least part of said boundary wall; a spatially non-uniform electric field (4) is generated between a first electrode or first plurality of electrodes (1, 301) located in the first environment and a second electrode or second plurality of electrodes (2, 302) located in the second environment, so that field lines of said non-uniform electric field cross said membrane, and a dielectrophoretic force generated on particles of said gaseous component (P) is at least part of a driving force of the permeation through said membrane, an amount of said product (P) being selectively removed from the first environment and collected in the second environment.

Process for producing ammonia synthesis gas

Multi-bed catalytic converter with inter-bed cooling

A multi-bed catalytic converter comprising at least a first catalytic bed, a second catalytic bed and a heat exchanger arranged between said first bed and said second bed, wherein said heat exchanger is arranged to transfer heat from the hot effluent of the first bed to a cooling medium; said heat exchanger comprises a plurality of stacked round plates, wherein adjacent plates define gaps therebetween, and the effluent of the first catalytic bed and the cooling medium are respectively fed into alternate gaps.

Process and equipment for the production of ammonia make-up syngas with an air separation unit as nitrogen source

A process and a plant for producing a makeup synthesis gas (6) for the synthesis of ammonia where a hydrocarbon feedstock is reformed in a primary reformer (10) and in an autothermal reformer (14) in parallel with said primary reformer; nitrogen is furnished by an air separation unit (13), and O 2 -enriched air (8) produced in said air separation unit is fed to the autothermal reformer. A method for the revamping of the front-end of an ammonia plant is also disclosed.

Process and reactors for selective removal of a product from a gaseous system

Process for revamping an ammonia plant with nitrogen-based washing of a purge stream

A process and a plant for producing ammonia, where an ASU (3) delivers an oxygen stream and a nitrogen stream; the oxygen stream (9) is fed to the secondary reformer of a front-end reforming section (1); the nitrogen stream (10) is used to wash a purge gas or tail gas taken from the synthesis loop (2), preferably in a cryogenic section; a methane-free and inert-free gas stream is recovered and recycled to the synthesis loop (2) or at the suction of the main syngas compressor, to recover the hydrogen contained therein. A corresponding method for increasing the capacity of an ammonia plant, by providing the ASU and feeding the oxygen stream to the secondary reformer and the nitrogen stream to a suitable purge gas recovery unit.

A perforated-tray column and a method of revamping the same

A perforated-tray column wherein each tray comprises downcomer pipes (6) for conveying a downwardly flowing liquid (L) to a next tray, wherein the downcomer pipe includes: a first portion (7) extending above the perforated tray, a second portion (8) extending below the perforated tray towards the next perforated tray, and an end guard (9) to prevent a gasous phase from entering the downward pipe.

Aqua-ammonia absorption refrigeration system

An aqua/ammonia absorption refrigeration process wherein: liquid ammonia is evaporated to produce ammonia vapors a refrigeration effect; ammonia vapors are absorbed in a lean aqueous solution of ammonia, obtaining a rich solution; gaseous ammonia is desorbed at high pressure from the rich solution to obtain gaseous ammonia and regenerate a lean solution; the gaseous ammonia is condensed and expanded to low pressure for further use in the evaporator, wherein the absorption step comprises: cooling and condensing a biphasic mixture of gaseous ammonia and lean solution in at least one evaporative condenser.

Process for producing ammonia synthesis gas

A method for increasing the capacity of an ammonia plant

A method for treatment of process condensate (1) in an ammonia plant, wherein the ammonia plant comprises a front-end section producing a make-up gas and a synthesis section where the make-up gas is reacted to ammonia, and said process condensate (1) is collected from one or more equipment of the ammonia plant and is an aqueous solution comprising ammonia,carbon dioxide and methanol. Said method comprises: stripping said process condensate with low-pressure steam (4), obtaining a vapour phase (5) comprising ammonia, carbon dioxide and methanol stripped from the process condensate; condensing said vapour phase, obtaining a solution (11) enriched of ammonia and methanol; re-introducing a first portion (12) of said solution to said stripping environment; recycling a second portion (13) of said solution to said ammonia plant.

A method for revamping an ammonia plant

A method for revamping an ammonia plant including a steam system, said steam system comprising at least a high-pressure section operating at a first pressure and a medium-pressure section operating at a second pressure lower than said first pressure, the revamping including: the provision of at least one additional heat recovery by means of a steam flow at a third pressure which is intermediate between said first and second pressure, and the provision of a steam export line arranged to export outside the ammonia plant at least a portion of said steam flow at said third pressure.

A method for the modernization of an ammonia plant

<p>UN MÉTODO PARA LA MODERNIZACIÓN DE UNA PLANTA DE AMONÍACO QUE INCLUYE UN SISTEMA DE VAPOR DE AGUA, DICHO SISTEMA DE VAPOR DE AGUA COMPRENDE POR LO MENOS UNA SECCIÓN DE PRESIÓN ALTA QUE OPERA A UNA PRIMERA PRESIÓN Y UNA SECCIÓN DE PRESIÓN MEDIA QUE OPERA A UNA SEGUNDA PRESIÓN MENOR QUE DICHA PRIMERA PRESIÓN, LA MODERNIZACIÓN INCLUYE: LA PROVISIÓN DE POR LO MENOS UNA RECUPERACIÓN DE CALOR ADICIONAL POR MEDIO DE UN FLUJO DE VAPOR DE AGUA A UNA TERCERA PRESIÓN LA CUAL ES INTERMEDIA ENTRE DICHA PRIMERA Y SEGUNDA PRESIÓN, Y LA PROVISIÓN DE UNA LÍNEA DE EXPORTACIÓN DE VAPOR DE AGUA QUE ESTÁ DISPUESTA PARA EXPORTAR HACIA FUERA DE LA PLANTA DE AMONIACO POR LO MENOS UNA PORCIÓN DE DICHO FLUJO DE VAPOR DE AGUA A DICHA TERCERA PRESIÓN.</p> <p> A METHOD FOR THE MODERNIZATION OF AN AMMONIA PLANT THAT INCLUDES A WATER VAPOR SYSTEM, SUCH WATER VAPOR SYSTEM INCLUDES AT LEAST A HIGH PRESSURE SECTION THAT OPERATES A FIRST PRESSURE AND A MEDIUM PRESSURE SECTION THAT OPERATES A SECOND PRESSURE LESS THAN SUCH FIRST PRESSURE, MODERNIZATION INCLUDES: THE PROVISION OF AT LEAST AN ADDITIONAL HEAT RECOVERY THROUGH A WATER VAPOR FLOW AT A THIRD PRESSURE WHICH IS INTERMEDIATE BETWEEN FIRST AND SECOND PRESSURE, AND THE PROVISION OF A WATER VAPOR EXPORT LINE THAT IS WILLING TO EXPORT OUTSIDE THE AMMONIA PLANT FOR AT LEAST ONE PORTION OF SUCH WATER VAPOR FLOW AT THIS THIRD PRESSURE. </p>

A perforated-tray column and a method of revamping the same

A perforated-tray column wherein each tray comprises downcomer pipes (6) for conveying a downwardly flowing liquid (L) to a next tray, wherein the downcomer pipe includes: a first portion (7) extending above the perforated tray, a second portion (8) extending below the perforated tray towards the next perforated tray, and an end guard (9) to prevent a gasous phase from entering the downward pipe.

A process for selective removal of a product from a gaseous system

A process for selective removal of a gaseous product (P) from a gaseous system comprising said product and other components (R1, R2), wherein the gaseous system is admitted to a first environment, which is separated from a second environment by a boundary wall, and a permeation membrane (3, 300) forms at least part of said boundary wall; a spatially non-uniform electric field (4) is generated between a first electrode or first plurality of electrodes (1, 301) located in the first environment and a second electrode or second plurality of electrodes (2, 302) located in the second environment, so that field lines of said non-uniform electric field cross said membrane, and a dielectrophoretic force generated on particles of said gaseous component (P) is at least part of a driving force of the permeation through said membrane, an amount of said product (P) being selectively removed from the first environment and collected in the second environment.

Process and plant to the production of methanol with improved distillation section

A process and a related plant for the synthesis of methanol, wherein a flash gas stream (103) obtained in the distillation section is treated to recycle the methanol contained therein and increase the production of refined methanol. Preferably the flash gas stream is washed with water in a counter-current column (C), recovering an acqueous solution of methanol (110) which is recycled back to the topping column (T) of the distillation section.

a method for renewing a co2 removal section for purification of a hydrogen containing gas

a presente invenção se refere a um método para renovação de uma seção de remoção de co2 para remoção de dióxido de carbono a partir de um gás de síntese contendo hidrogênio, em que a seção de remoção de co2 compreende uma seção de absorção (2) em que dióxido de carbono é transferido para uma solução de absorção e a uma torre de extração (stripping) (3) para regeneração da solução carregada de co2, referida torre de extração compreendendo uma zona superior (4) onde uma primeira corrente gasosa (10) contendo co2 e uma solução semi empobrecida parcialmente regenerada (11) são produzidas, e uma zona inferior (5) atuando como uma zona de extração onde uma segunda corrente gasosa (12) contendo co2 e uma solução regenerada empobrecida são produzidas, a segunda corrente de co2 (12) sendo uma corrente substancialmente pura contendo menos hidrogênio e impurezas do que a primeira corrente de co2. em concordância com a presente invenção, o método de renovação de uma seção de remoção de co2 proporciona a instalação de recursos de vedação (16) no interior da torre de extração (3), dispostos para isolar referida segunda corrente gasosa de co2 (12) a partir da primeira corrente (10), de maneira tal que a segunda corrente (12) pode ser exportada separadamente. The present invention relates to a method for renewing a carbon dioxide removal section for removal of carbon dioxide from a hydrogen containing synthesis gas, wherein the CO2 removal section comprises an absorption section (2) in that carbon dioxide is transferred to an absorption solution and a stripping tower (3) for regeneration of the co2 charged solution, said extraction tower comprising an upper zone (4) where a first gas stream (10) containing co2 and a partially regenerated semi-depleted solution (11) are produced, and a lower zone (5) acting as an extraction zone where a second gaseous stream (12) containing co2 and a depleted regenerated solution is produced, the second co2 (12) being a substantially pure stream ...

A process and a reactor for selective removal of a product from a gaseous system

A process for selective removal of a gaseous product (P) from a gaseous system comprising said product and other components (R1, R2), wherein the gaseous system is admitted to a first environment, which is separated from a second environment by a boundary wall, and a permeation membrane (3, 300) forms at least part of said boundary wall; a spatially non-uniform electric field (4) is generated between a first electrode or first plurality of electrodes (1, 301) located in the first environment and a second electrode or second plurality of electrodes (2, 302) located in the second environment, so that field lines of said non-uniform electric field cross said membrane, and a dielectrophoretic force generated on particles of said gaseous component (P) is at least part of a driving force of the permeation through said membrane, an amount of said product (P) being selectively removed from the first environment and collected in the second environment.

Process for producing ammonia synthesis gas

A process for producing ammonia synthesis gas from a hydrocarbon-containing feedstock, with steps of primary reforming, secondary reforming with an oxidant stream, and further treatment of the synthesis gas including shift, removal of carbon dioxide and methanation, wherein the synthesis gas delivered by secondary reforming is subject to a medium-temperature shift (MTS) at a temperature between 200 and 350°C, and primary reforming is operated with a steam-to-carbon ratio lower than 2. A corresponding method for revamping an ammonia plant is disclosed, where an existing HTS reactor is modified to operate at medium temperature, or replaced with a new MTS reactor, and the steam-to-carbon ratio in the primary reformer is lowered to a value in the range 1.5 ¨ 2, thus reducing inert steam in the flow rate through the equipments of the front-end.

Process for the production of ammonia synthesis gas from a feed stream containing hydrocarbons, which comprises subjecting the synthesis gas produced by the secondary reformation to medium temperature displacement between 200 and 350ºc, carrying out the primary reformation to a vapor / carbon ratio less than 2, and carry out a preforming step.

Proceso para la producción de gas de síntesis de amoníaco a partir de una corriente de alimentación que contiene hidrocarburos, que comprende someter el gas de síntesis producido por la reformación secundaria a desplazamiento de temperatura media entre 200 y 350 ºC, llevar a cabo la reformación primaria a una relación vapor/carbono menor a 2, y llevar a cabo un paso de preformado. Process for the production of ammonia synthesis gas from a feed stream containing hydrocarbons, which comprises subjecting the synthesis gas produced by the secondary reformation to medium temperature displacement between 200 and 350 ° C, carrying out the primary reformation at a vapor / carbon ratio of less than 2, and carry out a preforming step.

A process for the synthesis of ammonia

A dual pressure process for the synthesis of ammonia from a make-up gas, wherein the make-up gas is reacted in two steps in series, the second step operating at a greater pressure than the first step,and wherein a portion of the effluent of the first step is recycled back to the first step, said portion containing unreacted make-up gas.

Improved horizontal radial flow reactor

A horizontal radial-flow reactor (1) comprising a horizontal reaction vessel (2) including an annular cylindrical reaction space (3) configured to contain a catalyst (4) for processing a gaseous flow, the reactor (1) comprising a plurality of gas permeable scallops (6) which surround said reaction space (3) and are arranged to distribute or collect said gaseous flow into or from said reaction space (3), wherein said gas permeable scallops (6) are distributed circumferentially around an outer boundary of the reaction space (3), including a gap in the array of scallops where shrinkage of the catalyst can occur while maintaining the symmetry of the catalyst distribution and a port in communication with said gap to load or unload a catalyst into or from said reaction space (3).

Craqueo de amoníaco para la producción de hidrógeno

Un proceso para la síntesis de hidrógeno mediante craqueo catalítico de amoníaco; el proceso comprende las etapas de someter una corriente que contiene amoníaco (10) a una etapa de craqueo catalítico (11) en presencia de calor para producir un gas quemado y una corriente craqueada térmicamente (14) que contiene nitrógeno, hidrógeno y posiblemente amoníaco residual y opcionalmente agua; el proceso además comprende los pasos de someter la corriente craqueada térmicamente a una etapa de recuperación de hidrógeno para producir una corriente de hidrógeno de alta pureza (22).

Method for controlling an ammonia or methanol converter

Method for controlling an ammonia synthesis converter or a methanol synthesis converter during intermittent availability of a renewable power-dependent hydrogen feed, wherein under a limited or no availability of power the converter effluent (20) is recycled back to the inlet of said converter in a loop, and heated5 to keep said converter in a hot stand-by mode wherein the temperature in the reaction space remains within a target range.

Process for ammonia synthesis using green hydrogen

Process for synthesis of ammonia wherein the synthesis of ammonia is performed in a high-pressure synthesis loop (101) which is partially fed with green hydrogen (26) produced from a renewable energy source and hydrogen recovered from a purge stream (21) of the loop is stored in a hydrogen storage (103) to compensate for temporary lack of the green hydrogen when the renewable energy source is not fully available.

Method for preparing a synthesis gas

Method for preparing a synthesis gas suitable for the synthesis of ammonia or methanol, the method comprises the step of feeding to the radiant portion of a primary reformer an oxygen-enriched air obtained by mixing air with an oxygen stream generated by water electrolysis.

Process for producing ammonia

A process for producing ammonia (2) in an ammonia synthesis converter (19) with co-production of steam (40) from the recovery of process heat generated in the synthesis converter, the process includes producing power (44) from expansion of said steam (40) in a steam turbine (42) which is mechanically coupled to a reversible motor/generator (43) and to a compressor so to form an assembly which can be selectively operated in a first mode of operation and in a second mode of operation wherein: in said first mode, mechanical power (44) is transferred from said steam turbine (42) to said reversible motor/generator (43) and to said compressor whilst in said second mode, mechanical power (44) is transferred to said compressor from said steam turbine (42) and from said reversible motor/generator.

Process for producing ammonia

A process for producing ammonia (2) in an ammonia synthesis converter (19) with co-production of steam (40) from the recovery of process heat generated in the synthesis converter, the process includes producing power (44) from expansion of said steam (40) in a steam turbine (42) which is mechanically coupled to a reversible motor/generator (43) and to a compressor so to form an assembly which can be selectively operated in a first mode of operation and in a second mode of operation wherein: in said first mode, mechanical power (44) is transferred from said steam turbine (42) to said reversible motor/generator (43) and to said compressor whilst in said second mode, mechanical power (44) is transferred to said compressor from said steam turbine (42) and from said reversible motor/generator.

Process for ammonia synthesis using green hydrogen

Process for synthesis of ammonia wherein the synthesis of ammonia is performed in a high-pressure synthesis loop (101) which is partially fed with green hydrogen (26) produced from a renewable energy source and hydrogen recovered from a purge stream (21) of the loop is stored in a hydrogen storage (103) to compensate for temporary lack of the green hydrogen when the renewable energy source is not fully available.

Craqueamento de amônia para a produção de hidrogênio

craqueamento de amônia para a produção de hidrogênio. a presente invenção se refere a um processo para a síntese de hidrogênio através do craqueamento catalítico de amônia; o processo compreende as etapas de submeter uma corrente contendo amônia (10) a uma etapa de craqueamento catalítico (11) na presença de calor para produzir um gás queimado e uma corrente de craqueamento térmico (14) contendo nitrogênio, hidrogênio e possivelmente amônia residual e opcionalmente água; o processo compreende ainda as etapas de submeter a corrente de craqueamento térmico a uma etapa de recuperação de hidrogênio para produzir uma corrente de hidrogênio de alta pureza (22).

Method for controlling a synthesis loop

A method for controlling a synthesis loop for production of a chemical product, such as ammonia or methanol, wherein a feed rate of the loop depends on at least one source of renewable energy, the pressure of the loop and the delivery rate of a makeup compressor and of a circulation compressor are continuously controlled to follow the variable rate of the feed while maintaining the loop pressure within a target deviation from a design loop pressure.

Method for preparing a synthesis gas

Method for preparing a synthesis gas suitable for the synthesis of ammonia or methanol, the method comprises the step of feeding to the radiant portion of a primary reformer an oxygen-enriched air obtained by mixing air with an oxygen stream generated by water electrolysis.

Metodo de preparacion de un gas de sintesis.

Se describe un método para preparar un gas de síntesis adecuado para la síntesis de amoníaco o metanol, el método comprende la etapa de alimentar la parte radiante de un reformador primario con aire enriquecido con oxígeno obtenido mezclando aire con una corriente de oxígeno generada por electrólisis del agua.

Process for ammonia synthesis using green hydrogen

Process for synthesis of ammonia wherein the synthesis of ammonia is performed in a high-pressure synthesis loop (101) which is partially fed with green hydrogen (26) produced from a renewable energy source and hydrogen recovered from a purge stream (21) of the loop is stored in a hydrogen storage (103) to compensate for temporary lack of the green hydrogen when the renewable energy source is not fully available.

Proceso para la sintesis de amoniaco utilizando hidrogeno verde

Proceso para la sintesis de amoniaco en donde la sintesis es llevada a cabo en un bucle (101) de sintesis a elevada presion que esta parcialmente alimentado con hidrogeno verde (26) producido a partir de una fuente de energia renovable y el hidrogeno recuperado a partir de una corriente de purga (21) del bucle es almacenado en un almacenamiento (103) de hidrogeno para compensar la falta temporaria del hidrogeno verde cuando la fuente de energia renovable no esta totalmente disponible.

Proceso para la síntesis de amoníaco utilizando hidrógeno verde

Proceso para la síntesis de amoníaco en donde la síntesis es llevada a cabo en un bucle (101) de síntesis a elevada presión que está parcialmente alimentado con hidrógeno verde (26) producido a partir de una fuente de energía renovable y el hidrógeno recuperado a partir de una corriente de purga (21) del bucle es almacenado en un almacenamiento (103) de hidrógeno para compensar la falta temporaria del hidrógeno verde cuando la fuente de energía renovable no está totalmente disponible.

Processo para síntese de amônia usando hidrogênio verde

processo para síntese de amônia usando hidrogênio verde. processo para síntese de amônia em que a síntese de amônia é realizada em um circuito de síntese de alta pressão (101) que é parcialmente alimentado com hidrogênio renovável (26) produzido a partir de uma fonte de energia renovável e hidrogênio recuperado a partir de um fluxo de purga (21) do circuito é armazenado em armazenamento de hidrogênio (103) para compensar a falta temporária de hidrogênio renovável quando a fonte de energia renovável não estiver totalmente disponível.

Proceso para la síntesis de amoníaco utilizando hidrógeno verde

Proceso para la síntesis de amoníaco en donde la síntesis es llevada a cabo en un bucle (101) de síntesis a elevada presión que está parcialmente alimentado con hidrógeno verde (26) producido a partir de una fuente de energía renovable y el hidrógeno recuperado a partir de una corriente de purga (21) del bucle es almacenado en un almacenamiento (103) de hidrógeno para compensar la falta temporaria del hidrógeno verde cuando la fuente de energía renovable no está totalmente disponible.

Process for ammonia synthesis using green hydrogen

Process for synthesis of ammonia wherein the synthesis of ammonia is performed in a high-pressure synthesis loop which is partially fed with green hydrogen produced from a renewable energy source and hydrogen recovered from a purge stream of the loop is stored in a hydrogen storage to compensate for temporary lack of the green hydrogen when the renewable energy source is not fully available.

Método para preparação de um gás de síntese

método para preparação de um gás de síntese. a presente invenção se refere a um método para preparação de um gás de síntese adequado para a síntese de amônia ou de metanol, o método compreendendo a etapa de alimentação para a porção radiante de um reformador primário de um ar enriquecido por oxigênio obtido por misturação de ar com uma corrente de oxigênio gerada por eletrólise de água.

Radial or axial-radial chemical reactor with a fine catalyst

reator qímico radial ou axial radial com um catalisador fino

A presente invenção se refere a um reator (1) para reações químicas catalíticas, compreendendo um leito catalítico (3) com uma forma anular cilíndrica atravessada por um fluxo radial ou fluxo axial radial misturado, em que o leito é delimitado por paredes cilíndricas (4, 5) feitas permeáveis a gás por intermédio de fendas (10) e o leito catalítico é formado por partículas de catalisador com um tamanho mínimo nominal (d) de maneira tal que a relação entre uma dimensão transversal das fendas e o tamanho mínimo nominal das partículas de catalisador é de menos do que ou igual a 0,6; o leito catalítico contém não mais do que 3% em peso de partículas com um tamanho efetivo menor do que referido tamanho nominal.

Radial or axial-radial chemical reactor with a fine catalyst

Reactor (1) for catalytic chemical reactions comprising a catalyst bed (3) with an annular-cylindrical form crossed by a radial flow or mixed axial-radial flow, wherein the bed is delimited by cylindrical walls (4, 5) made gas-permeable by means of slits (10) and the catalyst bed is formed by particles of catalyst with a nominal minimum size (d ) such that:the ratio between a transverse dimension of the slits and the nominal minimum size of the particles of catalyst is smaller than or equal to 0.6; the catalyst bed contains no more than 3% by weight of particles with an actual size smaller than said nominal size.

Reator para reações químicas catalíticas e método para carregamento de catalisador para tal reator

a presente invenção se refere a um reator (1) para reações químicas catalíticas, compreendendo um leito catalítico (3) com uma forma anular cilíndrica atravessada por um fluxo radial ou fluxo axial radial misturado, em que o leito é delimitado por paredes cilíndricas (4, 5) feitas permeáveis a gás por intermédio de fendas (10) e o leito catalítico é formado por partículas de catalisador com um tamanho mínimo nominal (d) de maneira tal que a relação entre uma dimensão transversal das fendas e o tamanho mínimo nominal das partículas de catalisador é de menos do que ou igual a 0,6; o leito catalítico contém não mais do que 3% em peso de partículas com um tamanho efetivo menor do que referido tamanho nominal.

Radial or axial-radial chemical reactor with a fine catalyst

Reactor (1) for catalytic chemical reactions comprising a catalyst bed (3) with an annular-cylindrical form crossed by a radial flow or mixed axial-radial flow, wherein the bed is delimited by cylindrical walls (4, 5) made gas-permeable by means of slits (10) and the catalyst bed is formed by particles of catalyst with a nominal minimum size (d ) such that:the ratio between a transverse dimension of the slits and the nominal minimum size of the particles of catalyst is smaller than or equal to 0.6; the catalyst bed contains no more than 3% by weight of particles with an actual size smaller than said nominal size.

Radial or axial-radial chemical reactor with a fine catalyst

Reactor (1) for catalytic chemical reactions comprising a catalyst bed (3) with an annular-cylindrical form crossed by a radial flow or mixed axial-radial flow, wherein the bed is delimited by cylindrical walls (4, 5) made gas-permeable by means of slits (10) and the catalyst bed is formed by particles of catalyst with a nominal minimum size (d ) such that:the ratio between a transverse dimension of the slits and the nominal minimum size of the particles of catalyst is smaller than or equal to 0.6; the catalyst bed contains no more than 3% by weight of particles with an actual size smaller than said nominal size.

Ammonia cracking for hydrogen production

A process for the synthesis of hydrogen via the catalytic cracking of ammonia; the process comprises the steps of subjecting an ammonia-containing stream (10) to a catalytic cracking step (11) in the presence of heat to yield a combusted gas and a thermally cracked stream (14) containing nitrogen, hydrogen and possibly residual ammonia and optionally water; the process further comprises the steps of subjecting the thermally cracked stream to a hydrogen recovery step to yield a high-purity hydrogen stream (22).

Improved horizontal radial flow reactor

A horizontal radial-flow reactor (1) comprising a horizontal reaction vessel (2) including an annular cylindrical reaction space (3) configured to contain a catalyst (4) for processing a gaseous flow, the reactor (1) comprising a plurality of gas permeable scallops (6) which surround said reaction space (3) and are arranged to distribute or collect said gaseous flow into or from said reaction space (3), wherein said gas permeable scallops (6) are distributed circumferentially around an outer boundary of the reaction space (3), including a gap in the array of scallops where shrinkage of the catalyst can occur while maintaining the symmetry of the catalyst distribution and a port in communication with said gap to load or unload a catalyst into or from said reaction space (3).

Ammonia cracking for hydrogen production

Process for production of hydrogen from ammonia, including ammonia cracking wherein ammonia is decomposed into hydrogen and nitrogen, wherein the ammonia cracking is performed in a sequence of cracking steps (13, 36, 17, 20) and a finally cracked stream (21) is obtained after a last cracking step (20), wherein the last ammonia cracking step (20) is performed adiabatically and/or the finally cracked stream (21) is quenched by direct mixing with water or steam after the last cracking step.

Multi-bed catalytic converter with inter-bed cooling

A multi-bed catalytic converter comprising at least a first catalytic bed, a second catalytic bed and a heat exchanger arranged between said first bed and said second bed, wherein said heat exchanger is arranged to transfer heat from the hot effluent of the first bed to a cooling medium; said heat exchanger comprises a plurality of stacked round plates, wherein adjacent plates define gaps therebetween, and the effluent of the first catalytic bed and the cooling medium are respectively fed into alternate gaps.

A process for production of hydrogen gas

A process for the production of a hydrogen-containing gas, such as ammonia make-up gas (19), from a hydrocarbon feed (15), the process comprising reforming of a first portion of a hydrocarbon feed, which is performed in a first reforming section (80) including a fired furnace (4) for primary reforming, and a parallel steam reforming process (10) of a second portion (17) of said hydrocarbon feed, which is performed in a second reforming section (8), to generate a hydrogen-rich fuel (22) for said fired furnace.

Method for preparing a synthesis gas

Method for controlling a synthesis loop

A method for controlling a synthesis loop for production of a chemical product, such as ammonia or methanol, wherein a feed rate of the loop depends on at least one source of renewable energy, the pressure of the loop and the delivery rate of a makeup compressor and of a circulation compressor are continuously controlled to follow the variable rate of the feed while maintaining the loop pressure within a target deviation from a design loop pressure.

Process for ammonia synthesis using green hydrogen

Process for synthesis of ammonia wherein the synthesis of ammonia is performed in a high-pressure synthesis loop (101) which is partially fed with green hydrogen (26) produced from a renewable energy source and hydrogen recovered from a purge stream (21) of the loop is stored in a hydrogen storage (103) to compensate for temporary lack of the green hydrogen when the renewable energy source is not fully available.

Método para controlar un bucle de síntesis

Un método para controlar un bucle de síntesis para la producción de un producto químico, tal como amoníaco o metanol, en donde un caudal de alimentación del bucle depende de al menos una fuente de energía renovable, la presión del bucle y el caudal de suministro del compresor de reposición y del compresor de circulación son continuamente controlados para seguir el caudal variable de la alimentación mientras se mantiene la presión del bucle dentro de una desviación diana a partir de la presión de bucle de diseño.

Process for ammonia synthesis using green hydrogen and method for revamping an ammonia plant

Process for synthesis of ammonia wherein: ammonia make-up gas (7) containing hydrogen and nitrogen is reacted in an ammonia converter (15) under ammonia forming conditions thus obtaining an ammonia-containing effluent (8); a first hydrogen portion contained in the ammonia make-up gas (7) is produced by reforming a hydrocarbon source (1) in a reforming process (100); a second hydrogen portion (19) contained in the ammonia make-up gas (7) is produced separately from said reforming process (100), by using at least a renewable energy source (SE, WE); a part of said hydrogen (19) produced in step (c) is stored in a hydrogen storage (103); hydrogen (20) from said hydrogen storage (103) is used to fully or partially replace said second hydrogen portion (19) when said renewable energy source (SE, WE) is fully or partially unavailable. Said process comprising the steps of: assessing an expected flow rate of the hydrogen (19) produced in step (c); adjusting a flow rate of the hydrocarbon source (1) so that a flow rate of the first hydrogen portion in said ammonia make- up gas (7) is in a desired ratio with respect to said expected flow rate; detecting an actual amount, e.g., a filling level, of said hydrogen in said hydrogen storage (103); detecting an actual flow rate of hydrogen produced using the renewable energy source (SE, WE), and adjusting a flow rate of the hydrogen (20) from said hydrogen storage (103) depending on said actual amount detected in said hydrogen storage (103) and on said actual flow rate.

Method for controlling an ammonia or methanol converter

Method for controlling an ammonia synthesis converter or a methanol synthesis converter during intermittent availability of a renewable power-dependent hydrogen feed, wherein under a limited or no availability of power the converter effluent (20) is recycled back to the inlet of said converter in a loop, and heated5 to keep said converter in a hot stand-by mode wherein the temperature in the reaction space remains within a target range.

Método para controlar un convertidor de amoníaco o metanol

Un método para controlar un convertidor de síntesis de amoníaco o un convertidor de síntesis de metanol durante la disponibilidad intermitente de una alimentación de hidrógeno dependiente de energía renovable, en donde bajo una limitada disponibilidad de energía o sin disponibilidad de ella, el efluente del convertidor (20) es reciclado de regreso a la entrada de dicho convertidor en un bucle, y se calienta para mantener dicho convertidor en un modo en espera caliente en donde la temperatura en el espacio de reacción se mantiene dentro de un rango diana.